CN115287275A - Method for purifying hyaluronidase - Google Patents
Method for purifying hyaluronidase Download PDFInfo
- Publication number
- CN115287275A CN115287275A CN202211108780.2A CN202211108780A CN115287275A CN 115287275 A CN115287275 A CN 115287275A CN 202211108780 A CN202211108780 A CN 202211108780A CN 115287275 A CN115287275 A CN 115287275A
- Authority
- CN
- China
- Prior art keywords
- hyaluronidase
- pressure
- low
- pressure ceramic
- membrane
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 108010003272 Hyaluronate lyase Proteins 0.000 title claims abstract description 156
- 102000001974 Hyaluronidases Human genes 0.000 title claims abstract description 154
- 229960002773 hyaluronidase Drugs 0.000 title claims abstract description 154
- 238000000034 method Methods 0.000 title claims abstract description 69
- 239000012528 membrane Substances 0.000 claims abstract description 164
- 239000000919 ceramic Substances 0.000 claims abstract description 142
- 239000007788 liquid Substances 0.000 claims abstract description 107
- 239000000243 solution Substances 0.000 claims abstract description 101
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 62
- 230000001954 sterilising effect Effects 0.000 claims abstract description 56
- 239000012535 impurity Substances 0.000 claims abstract description 38
- 238000000855 fermentation Methods 0.000 claims abstract description 37
- 230000004151 fermentation Effects 0.000 claims abstract description 37
- 239000000337 buffer salt Substances 0.000 claims abstract description 28
- 238000004519 manufacturing process Methods 0.000 claims abstract description 23
- KIUKXJAPPMFGSW-DNGZLQJQSA-N (2S,3S,4S,5R,6R)-6-[(2S,3R,4R,5S,6R)-3-Acetamido-2-[(2S,3S,4R,5R,6R)-6-[(2R,3R,4R,5S,6R)-3-acetamido-2,5-dihydroxy-6-(hydroxymethyl)oxan-4-yl]oxy-2-carboxy-4,5-dihydroxyoxan-3-yl]oxy-5-hydroxy-6-(hydroxymethyl)oxan-4-yl]oxy-3,4,5-trihydroxyoxane-2-carboxylic acid Chemical compound CC(=O)N[C@H]1[C@H](O)O[C@H](CO)[C@@H](O)[C@@H]1O[C@H]1[C@H](O)[C@@H](O)[C@H](O[C@H]2[C@@H]([C@@H](O[C@H]3[C@@H]([C@@H](O)[C@H](O)[C@H](O3)C(O)=O)O)[C@H](O)[C@@H](CO)O2)NC(C)=O)[C@@H](C(O)=O)O1 KIUKXJAPPMFGSW-DNGZLQJQSA-N 0.000 claims abstract description 19
- 241000545744 Hirudinea Species 0.000 claims abstract description 19
- 229920002674 hyaluronan Polymers 0.000 claims abstract description 19
- 229960003160 hyaluronic acid Drugs 0.000 claims abstract description 19
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 96
- 102000004190 Enzymes Human genes 0.000 claims description 72
- 108090000790 Enzymes Proteins 0.000 claims description 72
- 229940088598 enzyme Drugs 0.000 claims description 72
- 230000000694 effects Effects 0.000 claims description 63
- 239000011780 sodium chloride Substances 0.000 claims description 49
- 239000000463 material Substances 0.000 claims description 30
- 239000012466 permeate Substances 0.000 claims description 25
- 241001052560 Thallis Species 0.000 claims description 20
- 238000013461 design Methods 0.000 claims description 6
- 239000000203 mixture Substances 0.000 claims description 3
- 239000007857 degradation product Substances 0.000 claims 1
- 238000009776 industrial production Methods 0.000 abstract description 6
- 150000003384 small molecules Chemical class 0.000 abstract description 3
- 230000000052 comparative effect Effects 0.000 description 41
- 238000004659 sterilization and disinfection Methods 0.000 description 38
- 238000005119 centrifugation Methods 0.000 description 25
- 238000001556 precipitation Methods 0.000 description 19
- 238000002156 mixing Methods 0.000 description 14
- 241000894006 Bacteria Species 0.000 description 11
- 239000002244 precipitate Substances 0.000 description 11
- 238000005070 sampling Methods 0.000 description 11
- 238000004140 cleaning Methods 0.000 description 8
- 238000001514 detection method Methods 0.000 description 8
- 238000000502 dialysis Methods 0.000 description 8
- 238000012545 processing Methods 0.000 description 6
- 238000000746 purification Methods 0.000 description 6
- 230000001580 bacterial effect Effects 0.000 description 5
- 239000012141 concentrate Substances 0.000 description 5
- 238000002474 experimental method Methods 0.000 description 5
- 238000012795 verification Methods 0.000 description 5
- 238000010924 continuous production Methods 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 238000012986 modification Methods 0.000 description 4
- 230000004048 modification Effects 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 3
- 238000001976 enzyme digestion Methods 0.000 description 3
- 239000011148 porous material Substances 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- 239000012487 rinsing solution Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 241000251539 Vertebrata <Metazoa> Species 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 2
- 239000000872 buffer Substances 0.000 description 2
- 229960001927 cetylpyridinium chloride Drugs 0.000 description 2
- YMKDRGPMQRFJGP-UHFFFAOYSA-M cetylpyridinium chloride Chemical compound [Cl-].CCCCCCCCCCCCCCCC[N+]1=CC=CC=C1 YMKDRGPMQRFJGP-UHFFFAOYSA-M 0.000 description 2
- 238000005202 decontamination Methods 0.000 description 2
- 230000003588 decontaminative effect Effects 0.000 description 2
- 238000005034 decoration Methods 0.000 description 2
- 238000005342 ion exchange Methods 0.000 description 2
- 108090000623 proteins and genes Proteins 0.000 description 2
- 239000006228 supernatant Substances 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 210000001550 testis Anatomy 0.000 description 2
- 239000002435 venom Substances 0.000 description 2
- 231100000611 venom Toxicity 0.000 description 2
- 210000001048 venom Anatomy 0.000 description 2
- 229920000936 Agarose Polymers 0.000 description 1
- CPELXLSAUQHCOX-UHFFFAOYSA-M Bromide Chemical compound [Br-] CPELXLSAUQHCOX-UHFFFAOYSA-M 0.000 description 1
- 241000238424 Crustacea Species 0.000 description 1
- 241000233866 Fungi Species 0.000 description 1
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 description 1
- 241000270322 Lepidosauria Species 0.000 description 1
- 241000270295 Serpentes Species 0.000 description 1
- 241000700605 Viruses Species 0.000 description 1
- 238000011095 buffer preparation Methods 0.000 description 1
- 239000007975 buffered saline Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 229940069078 citric acid / sodium citrate Drugs 0.000 description 1
- 238000012258 culturing Methods 0.000 description 1
- 230000000593 degrading effect Effects 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- CBMPTFJVXNIWHP-UHFFFAOYSA-L disodium;hydrogen phosphate;2-hydroxypropane-1,2,3-tricarboxylic acid Chemical compound [Na+].[Na+].OP([O-])([O-])=O.OC(=O)CC(O)(C(O)=O)CC(O)=O CBMPTFJVXNIWHP-UHFFFAOYSA-L 0.000 description 1
- 239000000975 dye Substances 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000005227 gel permeation chromatography Methods 0.000 description 1
- 239000008103 glucose Substances 0.000 description 1
- 150000004676 glycans Chemical class 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 210000003734 kidney Anatomy 0.000 description 1
- 210000004185 liver Anatomy 0.000 description 1
- 210000004324 lymphatic system Anatomy 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 210000000056 organ Anatomy 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 125000000913 palmityl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 description 1
- 229920001282 polysaccharide Polymers 0.000 description 1
- 239000005017 polysaccharide Substances 0.000 description 1
- 238000005185 salting out Methods 0.000 description 1
- 210000003491 skin Anatomy 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000003892 spreading Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000004094 surface-active agent Substances 0.000 description 1
- 238000010257 thawing Methods 0.000 description 1
- 239000003053 toxin Substances 0.000 description 1
- 231100000765 toxin Toxicity 0.000 description 1
- 108700012359 toxins Proteins 0.000 description 1
- 229960005486 vaccine Drugs 0.000 description 1
- 238000005303 weighing Methods 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12N—MICROORGANISMS OR ENZYMES; COMPOSITIONS THEREOF; PROPAGATING, PRESERVING, OR MAINTAINING MICROORGANISMS; MUTATION OR GENETIC ENGINEERING; CULTURE MEDIA
- C12N9/00—Enzymes; Proenzymes; Compositions thereof; Processes for preparing, activating, inhibiting, separating or purifying enzymes
- C12N9/14—Hydrolases (3)
- C12N9/24—Hydrolases (3) acting on glycosyl compounds (3.2)
- C12N9/2402—Hydrolases (3) acting on glycosyl compounds (3.2) hydrolysing O- and S- glycosyl compounds (3.2.1)
- C12N9/2474—Hyaluronoglucosaminidase (3.2.1.35), i.e. hyaluronidase
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P19/00—Preparation of compounds containing saccharide radicals
- C12P19/26—Preparation of nitrogen-containing carbohydrates
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12Y—ENZYMES
- C12Y302/00—Hydrolases acting on glycosyl compounds, i.e. glycosylases (3.2)
- C12Y302/01—Glycosidases, i.e. enzymes hydrolysing O- and S-glycosyl compounds (3.2.1)
- C12Y302/01035—Hyaluronoglucosaminidase (3.2.1.35), i.e. hyaluronidase
Landscapes
- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Engineering & Computer Science (AREA)
- Zoology (AREA)
- Wood Science & Technology (AREA)
- Genetics & Genomics (AREA)
- Bioinformatics & Cheminformatics (AREA)
- General Health & Medical Sciences (AREA)
- Biochemistry (AREA)
- General Engineering & Computer Science (AREA)
- Microbiology (AREA)
- Biotechnology (AREA)
- Molecular Biology (AREA)
- Biomedical Technology (AREA)
- Medicinal Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Enzymes And Modification Thereof (AREA)
Abstract
The invention provides a method for purifying hyaluronidase, which comprises the following steps: a) Sterilizing the hyaluronidase fermentation broth by using a plate frame to obtain a hyaluronidase clear liquid; b) Sterilizing the hyaluronidase clear liquid by adopting a low-pressure ceramic membrane to obtain hyaluronidase liquid treated by the low-pressure ceramic membrane; c) And removing impurities from the hyaluronidase liquid treated by the low-pressure ceramic membrane by using a high-pressure ceramic ultrafiltration membrane to obtain the hyaluronidase. According to the invention, the leech hyaluronidase is subjected to plate frame, (low pressure) ceramic membrane, (high pressure) ceramic ultrafiltration membrane process and certain concentration buffer salt solution feeding mode in sequence to reduce thallus and small molecule impurities in the hyaluronidase fermentation liquor, the process is low in production cost, is used for continuously producing enzyme-digested ultra-small molecule hyaluronic acid, does not introduce extra impurities, improves the quality of enzyme-digested ultra-small molecule hyaluronic acid products, and is suitable for large-scale industrial production.
Description
Technical Field
The invention relates to the technical field of purification methods, in particular to a method for purifying hyaluronidase.
Background
Hyaluronidase (HAase), also known as hyaluronidase, is a generic term for an enzyme class that specifically hydrolyzes hyaluronic acid.
Hyaluronidase is a generic term for a class of enzymes that are capable of degrading hyaluronic acid. Duran Reynals discovered a "spreading factor" in the 1928 study of extracts of mammalian testis and other tissues that promoted better spreading of subcutaneously injected vaccines, dyes, toxins, etc. Meyer in 1940 named this "diffusion factor" Hyaluronidase. Thereafter, hyaluronidase was detected in many tissues and organisms, including bacterial viruses, bacteria, fungi, etc., and also produced in the venom of non-vertebrates such as leeches and crustaceans. In vertebrates, hyaluronidase is found in the venom of snakes and lizards, and in the testis and other organs such as the liver, kidney, lymphatic system and skin.
The patent CN201410007408.1 discloses a hyaluronidase coding gene and a fermentation production and purification method thereof, the patent adopts an experimental-grade centrifugal sterilization and ion exchange method to purify leech hyaluronidase, and the method has the advantages of more reagents, more solvents, complex process and slow production efficiency, and is not suitable for preparing enzyme-digested ultra-small molecular hyaluronic acid in industrial production.
In the prior art, the purified leech hyaluronidase mostly adopts the traditional industrial methods such as plate frame sterilization, salting-out method, inorganic ceramic membrane sterilization, ion exchange method, gel chromatography, organic ultrafiltration (three or more), and the like, so that the enzyme activity yield is low, the process is complicated, the production cost is high, the efficiency is low, and the method is not suitable for the industrial continuous production of enzyme-digested ultra-small molecular hyaluronic acid.
Disclosure of Invention
In view of the above, the technical problem to be solved by the present invention is to provide a method for purifying hyaluronidase, which has high enzyme activity and does not introduce additional impurities.
The invention provides a method for purifying hyaluronidase, which comprises the following steps:
a) Sterilizing the hyaluronidase fermentation broth by using a plate frame to obtain a hyaluronidase clear liquid;
b) Sterilizing the hyaluronidase clear liquid by adopting a low-pressure ceramic membrane to obtain hyaluronidase liquid treated by the low-pressure ceramic membrane;
c) And (3) removing impurities from the hyaluronidase solution treated by the low-pressure ceramic membrane by using a high-pressure ceramic ultrafiltration membrane to obtain the hyaluronidase.
Preferably, the source of hyaluronidase of step a) is leech; the mass content of thalli in the hyaluronidase fermentation broth is 50-55 wt%.
Preferably, the mass content of the thalli in the hyaluronidase clear liquid in the step A) is 1 to 5 percent by weight;
the enzyme activity of the hyaluronidase clear liquid is 1.2 multiplied by 10 6 ～1.6×10 6 U/ml。
Preferably, the specification of the low-pressure ceramic membrane in the step B) is 50-200 nm; the membrane area of the low-pressure ceramic membrane is 0.286m 2 The design pressure of the equipment is 0.3-0.35 Mpa, and the temperature of the feed liquid is 30-35 ℃.
Preferably, after the low-pressure ceramic membrane is sterilized in the step B), adding buffer salt in a continuous flow adding manner, and dialyzing to obtain hyaluronic acid enzyme liquid treated by the low-pressure ceramic membrane; the enzyme activity of the hyaluronidase liquid treated by the low-pressure ceramic membrane is 5 multiplied by 10 5 ～7×10 5 U/ml; the buffer salt is 1-3% sodium chloride solution.
Preferably, the specification of the high-pressure ceramic ultrafiltration membrane in the step C) is 15000-25000 Da;
the membrane area of the high-pressure ceramic ultrafiltration membrane is 0.286m 2 The design pressure of the equipment is 0.5-0.9 Mpa, the pressure in the operation of the equipment is 0.70-0.75 Mpa, and the temperature of the feed liquid is 30-35 ℃.
Preferably, after the high-pressure ceramic membrane in the step C) is subjected to impurity removal, adding buffer salt in a continuous flow adding manner, and dialyzing until the tail line of the permeation solution is consistent with the concentration of the buffer salt solution, and then continuously adding the permeation solution in a flowing manner until the permeation solution is colorless to obtain the product; the buffer salt is 1-3% sodium chloride solution.
Preferably, the specification of the low-pressure ceramic membrane is 200nm.
Preferably, the high-pressure ceramic membrane has a specification of 15000Da.
The invention provides hyaluronidase which is prepared by the preparation method of any one of the technical schemes.
Compared with the prior art, the invention provides a method for purifying hyaluronidase, which comprises the following steps: a) Sterilizing the hyaluronidase fermentation broth by using a plate frame to obtain a hyaluronidase clear liquid; b) Sterilizing the hyaluronidase clear liquid by adopting a low-pressure ceramic membrane to obtain hyaluronidase liquid treated by the low-pressure ceramic membrane; c) And removing impurities from the hyaluronidase liquid treated by the low-pressure ceramic membrane by using a high-pressure ceramic ultrafiltration membrane to obtain the hyaluronidase. According to the invention, the leech hyaluronidase is subjected to plate frame, (low pressure) ceramic membrane, (high pressure) ceramic ultrafiltration membrane process and certain concentration buffer salt solution feeding mode in sequence to reduce thallus and small molecule impurities in the hyaluronidase fermentation liquor, the process is low in production cost, is used for continuously producing enzyme-digested ultra-small molecule hyaluronic acid, does not introduce extra impurities, improves the quality of enzyme-digested ultra-small molecule hyaluronic acid products, and is suitable for large-scale industrial production.
Drawings
FIG. 1 is a diagram of hyaluronidase fermentation broth after centrifugation in example 1 of the present invention;
FIG. 2 is a diagram showing the clear liquid of hyaluronidase of example 1 of the present invention after centrifugation;
FIG. 3 is a diagram of the hyaluronidase solution after low pressure ceramic membrane treatment in example 1 of the present invention after centrifugation;
FIG. 4 is a diagram of a purified hyaluronidase solution in example 1 of the present invention.
Detailed Description
The invention provides a method for purifying hyaluronidase, and the method can be realized by appropriately modifying process parameters by one skilled in the art according to the content in the text. It is expressly intended that all such similar substitutes and modifications apparent to those skilled in the art are deemed to be within the scope of the invention. While the methods and applications of this invention have been described in terms of preferred embodiments, it will be apparent to those of ordinary skill in the art that variations and modifications in the methods and applications described herein, as well as other suitable variations and combinations, may be made to implement and use the techniques of this invention without departing from the spirit and scope of the invention.
The invention provides a method for purifying hyaluronidase, which comprises the following steps:
a) Performing plate-frame sterilization on hyaluronidase fermentation broth to obtain hyaluronidase clear liquid;
b) Sterilizing the hyaluronidase clear liquid by adopting a low-pressure ceramic membrane to obtain hyaluronidase liquid treated by the low-pressure ceramic membrane;
c) And removing impurities from the hyaluronidase liquid treated by the low-pressure ceramic membrane by using a high-pressure ceramic ultrafiltration membrane to obtain the hyaluronidase.
The invention provides a method for purifying hyaluronidase, which is characterized in that hyaluronidase fermentation liquor is subjected to plate-and-frame sterilization to obtain hyaluronidase clear liquid.
The source of the hyaluronidase fermentation broth of the present invention is not limited thereto, and those skilled in the art can easily understand that the hyaluronidase fermentation is preferably carried out by using patent CN201410007408.1 (a hyaluronidase encoding gene and its fermentation production and purification method). Sources of hyaluronidase are: leech source.
The invention preferably adopts the following modes to carry out the detection of the activity of the hyaluronidase:
definition of hyaluronidase activity units: the amount of enzyme required to release 1ug of glucose reducing equivalents of reducing sugar from hyaluronic acid per hour at pH5.5 and 38 ℃ is one enzyme activity unit.
The hyaluronidase activity was measured by plate clearing circle method and CTAB (Hexadecyl trimetyl amonium Bromide) turbidity method: hyaluronic acid is macromolecular polysaccharide, and is precipitated in a surfactant aqueous solution with a certain concentration, and hydrolyzed low-molecular-weight oligomeric HA cannot be precipitated. By using the principle, the activity of the hyaluronidase can be quickly and simply identified.
Buffer preparation (50 mM citric acid/sodium citrate pH5.3, 150mM NaCl, 0.02%) 3 N), 50ml of buffer was measured, 1.5% agarose and 1mg/ml HA were added, and plates were prepared after thawing. Dripping the fermentation liquid into the inside of the pore diameter, and culturing the flat plate at 37 DEG C10h, covering a proper amount of 10% (w/v) cetylpyridinium chloride (cetylpyridinium chloride) aqueous solution on the flat plate, and forming a transparent ring after about 10-20min, as shown in the invention, and shown in figure 2. The CTAB turbidity method detects the hyaluronidase activity. In a 1ml reaction system, 100. Mu.l of HA (2 mg/ml) was added to 1ml of a fermentation broth supernatant or an appropriate amount of an enzyme solution, pH5.5, and 50mM of a citric acid-disodium hydrogenphosphate buffer. After mixing, the mixture was placed in a 38 ℃ water bath to react for 30min, 2ml of CTAB (2.5 g/L) was immediately added to react for 5min at room temperature, and turbidity comparative measurement was performed at 400 nm.
And (3) degerming the leech hyaluronidase fermentation liquor by adopting a plate frame. The mass content of thalli in the hyaluronidase fermentation broth is 50-55 wt%.
Because the leech hyaluronidase fermentation liquor has high thallus content, compared with a centrifuge, the industrial process combining plate frame and inorganic ceramic membrane sterilization has the advantages of low equipment investment cost, low operation energy consumption and good sterilization effect compared with one or two inorganic ceramic membrane processes.
Performing plate-frame sterilization on hyaluronidase fermentation broth to obtain hyaluronidase clear liquid; the mass content of the thalli in the hyaluronidase clear liquid is 1-5 wt%; the enzyme activity of the hyaluronidase clear liquid is 1.2 multiplied by 10 6 ～1.6×10 6 U/ml。
Wherein the thallus content is determined as wet thallus content (detection method, using centrifuge rotation speed of 10000rpm/min and time of 15min as standard, weighing and calculating thallus to obtain the content, the method is designed for judging pure plate and frame bacteria effect). And (4) detecting the enzyme activity of the hyaluronidase clear liquid after plate frame sterilization.
And (4) degerming the hyaluronidase clear liquid by adopting a low-pressure ceramic membrane to obtain the hyaluronidase liquid treated by the low-pressure ceramic membrane.
The specification of the low-pressure ceramic membrane is 50-200 nm, and the membrane area is 0.286m 2 The specification of the low-pressure ceramic membrane is 50-200 nm, and the specification is 50nm and 200nm.
Sterilizing the fermented hyaluronidase clear liquid after plate frame sterilization by using the inorganic ceramic membrane, wherein the pressure of the low-pressure ceramic membrane is 0.3-0.35 Mpa; the pressure is selected to be the best stability of the low-pressure ceramic membrane treatment material in the industry, the method is suitable for industrial production, and the temperature of the material liquid is controlled to be 30-35 ℃ in the operation of equipment (the normal fluctuation range of temperature control in the operation of the equipment).
After the low-pressure ceramic membrane is sterilized, adding buffer salt in a continuous flow adding mode, and dialyzing to obtain hyaluronidase liquid treated by the low-pressure ceramic membrane; the buffer salt is 1-3% sodium chloride solution.
The method comprises the following specific steps: concentrating by 3 times (1/3 of the clear hyaluronidase solution after plate frame sterilization) with inorganic ceramic membrane, adding buffer salt, and adopting continuous flow addition;
dialyzing to obtain total hyaluronidase clear liquid, centrifuging the clear liquid, determining whether there is no macroscopic thallus precipitate, and determining the enzyme activity of clear liquid containing hyaluronidase to be 5 × 10 5 ～7×10 5 U/ml; (volume is 2 times of the clear liquid after plate frame sterilization).
And removing impurities from the hyaluronidase liquid treated by the low-pressure ceramic membrane by using a high-pressure ceramic ultrafiltration membrane to obtain the hyaluronidase.
The ceramic ultrafiltration membrane has the greatest characteristics of long service life, tiny pore diameter, capability of filtering and intercepting tiny organic matters, capability of separating at normal temperature, low energy consumption and high water utilization rate.
After the low-pressure ceramic membrane is degerming, reducing the content of small molecular impurities by using a 15000-25000Da high-pressure ceramic ultrafiltration membrane; the high pressure ceramic membrane includes, but is not limited to, 15000, 25000Da two membranes.
The inventor finds that when the hyaluronidase liquid is treated under the same condition, the treatment capacity of the ceramic ultrafiltration membrane is more stable, and the hyaluronic acid membrane has the advantages of long service life, pollution resistance, organic solvent resistance, stable operation and the like.
The operation pressure is 0.70Mpa, the designed membrane area of the high-pressure ceramic ultrafiltration membrane is about 0.286m 2 . The high-pressure ceramic ultrafiltration membrane equipment has the design pressure of 0.5-0.9 Mpa, the pressure of 0.70-0.75 Mpa in the operation of the equipment, and the pressure is in a normal fluctuation range, and the pressure is selected to be the best stability of the high-pressure ceramic membrane treatment material in the industry, so that the high-pressure ceramic ultrafiltration membrane equipment is suitable for industrial production. The temperature of the feed liquid is 30-35 ℃ during the operation of the equipment (the normal fluctuation range of the temperature control during the operation of the equipment).
After the high-pressure ceramic membrane is subjected to impurity removal, adding buffer salt in a continuous flow adding mode, dialyzing until the concentration of a tail line of the permeation solution is consistent with that of the buffer salt solution, and continuously adding the permeation solution until the permeation solution is colorless; the buffer salt is 1-3% of sodium chloride solution; the method specifically comprises the following steps: continuously adding a sodium chloride solution after the material is concentrated, dialyzing until the tail line of the permeated solution is consistent with the concentration of a buffer salt solution (detected by a refractometer), continuously adding the sodium chloride solution until the permeated solution is colorless, collecting the concentrated solution, adding the sodium chloride solution, uniformly mixing (keeping the volume of the hyaluronidase solution consistent with that of the hyaluronidase solution after plate-frame sterilization, and detecting the activity of the hyaluronidase without macroscopic thalli precipitation after centrifugation).
The design pressure of the high-pressure ceramic ultrafiltration membrane equipment is 0.5-0.9 Mpa, the pressure of the equipment in operation is 0.70-0.75 Mpa, and the temperature of the feed liquid is 30-35 ℃.
The method can effectively improve the enzyme activity yield, does not introduce additional impurities, has simple operation, controllable process and low production cost, and is suitable for the industrial continuous production of the enzyme-digested ultra-small molecular hyaluronic acid.
The invention provides hyaluronidase which is prepared by the preparation method of any one of the technical schemes.
The preparation method of the invention has already been clearly described, and the details are not repeated.
The invention provides a method for purifying hyaluronidase, which comprises the following steps: a) Performing plate-frame sterilization on hyaluronidase fermentation broth to obtain hyaluronidase clear liquid; b) Sterilizing the hyaluronidase clear liquid by adopting a low-pressure ceramic membrane to obtain hyaluronidase liquid treated by the low-pressure ceramic membrane; c) And removing impurities from the hyaluronidase liquid treated by the low-pressure ceramic membrane by using a high-pressure ceramic ultrafiltration membrane to obtain the hyaluronidase. According to the invention, the leech hyaluronidase is subjected to plate frame, (low pressure) ceramic membrane, (high pressure) ceramic ultrafiltration membrane process and certain concentration buffer salt solution feeding mode in sequence to reduce thallus and small molecule impurities in the hyaluronidase fermentation liquor, the process is low in production cost, is used for continuously producing enzyme-digested ultra-small molecule hyaluronic acid, does not introduce extra impurities, improves the quality of enzyme-digested ultra-small molecule hyaluronic acid products, and is suitable for large-scale industrial production.
To further illustrate the present invention, a method for purifying hyaluronidase provided by the present invention is described in detail below with reference to examples.
Example 1
(1) Leech hyaluronidase fermentation broth plate-and-frame sterilization
Stirring 280L fermentation broth, collecting 140L fermentation broth (cell content of 100ML fermentation broth after centrifugation is 50%), sterilizing by plate-frame method, collecting 66L hyaluronidase clear liquid (cell content of 100ML clear liquid after centrifugation is 3.7%), sterilizing by plate-frame method, and collecting 1.38 × 10% hyaluronidase 6 U/ml。
(2) Low pressure ceramic membrane sterilization
Sterilizing 66L of hyaluronidase clear solution after taking pure bacteria of a plate frame by using a 200nm low-pressure ceramic membrane device, controlling the operating pressure to be 0.32Mpa, controlling the temperature of feed liquid to be 30-35 ℃, adding 2% sodium chloride solution when the material is concentrated by about 3 times, continuously adding the sodium chloride solution when the tail line of dialysis is consistent with the refraction of the 2% sodium chloride solution, stopping the machine when the total permeate solution is 132L, stopping the machine for cleaning the equipment, wherein the total treatment time is about 136min, uniformly mixing 132L of total permeate solution, sampling and detecting (no macroscopic bacteria precipitation exists after centrifugation, the enzyme activity of hyaluronidase is 6.32 multiplied by 10, the enzyme activity is 6.32L 5 U/ml)。
(3) High pressure ceramic ultrafiltration membrane decontamination
Removing impurities from 132L of hyaluronidase clear solution subjected to 200nm low-pressure ceramic membrane sterilization by using a 15000Da high-pressure ceramic ultrafiltration membrane, controlling the operating pressure to be 0.7Mpa, controlling the temperature of feed liquid to be 30-35 ℃, adding 2% sodium chloride solution when the material concentrated permeate liquid is 25L, continuously adding the sodium chloride solution in a flowing manner when the tail line of dialysis is consistent with the refraction of the 2% sodium chloride solution, continuously adding the sodium chloride solution in a flowing manner until the permeate liquid has no visible color, collecting 148L of the collected permeate liquid for sampling and detecting enzyme activity, collecting the concentrated liquid, adding 2% sodium chloride solution for rinsing twice, mixing the concentrated liquid and the rinsing liquid to 66L, stopping cleaning the equipment, wherein the total treatment time is about 274min, uniformly mixing and sampling and detecting 66L of total concentrated liquid (no visible precipitate after centrifugation, the enzyme activity of the 148L of the total permeate liquid is 24864U/ml, and the enzyme activity of the 66L of the total concentrated liquid hyaluronidase is 1.08 multiplied by 10, and the enzyme activity of the 66L of the total concentrated liquid is 1.08 multiplied by 10 6 No visible precipitate after U/ml centrifugation).
Proved by verification, 140L of leech hyaluronidase fermentation liquor is prepared into purified hyaluronidase liquor (no visible thalli after centrifugation) by the process, and the enzyme activity is 1.08 multiplied by 10 6 U/ml (the enzyme activity loss is about 22%, the enzyme activity detection value is detected under the same condition), the low-pressure ceramic membrane processing time is about 136min, and the high-pressure ceramic ultrafiltration membrane processing time is about 274min.
Example 2
(1) Leech hyaluronidase fermentation broth plate-and-frame sterilization
Collecting 147L fermentation broth (cell content of 100ML fermentation broth after centrifugation is 53%), sterilizing by plate frame, collecting hyaluronidase clear liquid (cell content of 100ML clear liquid after centrifugation is 4.6%), and sterilizing by plate frame, wherein the hyaluronidase clear liquid content is 1.53 × 10 6 U/ml。
(2) Low pressure ceramic membrane sterilization
Sterilizing the 69L fermented hyaluronidase clear liquid after taking the plate frame pure bacteria by using a 200nm inorganic ceramic membrane device, controlling the operating pressure to be 0.7Mpa, controlling the temperature of the feed liquid to be 30-35 ℃, adding 2% sodium chloride solution to continuously flow and dialyze when the material is concentrated by 3 times, continuously flowing and adding the sodium chloride solution when the tail line of the dialysis is consistent with the refraction of the 2% sodium chloride solution, stopping the machine when the total permeate liquid is 138L, stopping the machine for cleaning, wherein the total treatment time is about 168min, uniformly mixing 138L total permeate liquid, sampling and detecting (no macroscopic bacteria precipitation exists after centrifugation, the enzyme activity of hyaluronidase is 6.96 multiplied by 10, the enzyme activity of the hyaluronidase is 138.96 multiplied by 10 5 U/ml)。
(3) High pressure ceramic ultrafiltration membrane decontamination
Removing impurities from 138L hyaluronidase clear solution subjected to sterilization by 200nm inorganic ceramic membrane by using a 25000Da high-pressure ceramic ultrafiltration membrane, controlling the operating pressure to be 0.7Mpa, controlling the temperature of feed liquid to be 30-35 ℃, adding 2% sodium chloride solution when the material concentrated permeate liquid is 25L, continuously adding the sodium chloride solution in a flowing manner for dialysis until the tail line is consistent with the refraction of the 2% sodium chloride solution, continuously adding the sodium chloride solution in a flowing manner until the permeate liquid has no visible color, collecting 154L permeate liquid in the concentrate, sampling and detecting enzyme activity, collecting the concentrate, adding 2% sodium chloride solution for rinsing twice, and adding the concentrate and the rinsing liquid for rinsing twiceMixing to 69L, stopping the cleaning equipment, collecting the total treatment time of 196min, mixing 69L total concentrate, sampling, and detecting (no visible precipitate after centrifugation, 154L total permeate hyaluronidase activity of 178920U/ml,69L total concentrate hyaluronidase activity of 9.37 × 10) 5 U/ml)。
It is verified that 147L of the leech hyaluronidase fermentation broth is used for preparing purified hyaluronidase liquid (no macroscopic thalli precipitation after centrifugation) by the process, and the enzyme activity is 9.37 multiplied by 10 5 U/ml (enzyme activity loss is about 39%, the enzyme activity detection value is obtained by detection under the same condition), the low-pressure ceramic membrane treatment time is about 168min, and the high-pressure ceramic ultrafiltration membrane treatment time is about 196min.
Example 3
(1) Leech hyaluronidase fermentation broth plate-and-frame sterilization
Taking 146L fermentation broth (the bacterial content of 100ML fermentation broth after centrifugation is 51%), taking 66L hyaluronidase clear liquid after plate-frame sterilization (the bacterial content of 100ML clear liquid after centrifugation is 3.4%), and taking 1.41 × 10% hyaluronidase content after plate-frame sterilization 6 U/ml。
(2) Low pressure ceramic membrane sterilization
Sterilizing 66L of fermented hyaluronidase clear liquid after taking plate frame pure bacteria by using 50nm inorganic ceramic membrane equipment, controlling the operating pressure to be 0.32Mpa, controlling the temperature of feed liquid to be 30-35 ℃, adding 2% sodium chloride solution when the material is concentrated by 3 times, continuously adding sodium chloride solution when the tail line is dialyzed until the refraction of the material is consistent with that of the 2% sodium chloride solution, continuously adding the sodium chloride solution when the tail line is dialyzed until the total permeate liquid is 132L, stopping the machine for cleaning the equipment when the total permeate liquid is added, wherein the total treatment time is about 246min, uniformly mixing 132L total permeate liquid, sampling and detecting (no macroscopic thallus precipitate exists after centrifugation, the hyaluronidase enzyme activity is 6.03 multiplied by 10, the total treatment time is 6.03 5 U/ml)。
(3) High pressure ceramic ultrafiltration membrane for impurity removal
Removing impurities from 50nm clear hyaluronidase solution 132L sterilized by inorganic ceramic membrane with high pressure of 15000Da by ceramic ultrafiltration membrane, controlling operation pressure at 0.7Mpa, material liquid temperature at 30-35 deg.C, adding 2% sodium chloride solution when material concentrated permeate liquid is 25L, dialyzing until tail line is consistent with refraction of 2% sodium chloride solution, and collecting the filtrateContinuously adding sodium chloride solution until the permeation solution has no visible color, collecting total permeation solution, sampling 160L, detecting enzyme activity, collecting concentrated solution, adding 2% sodium chloride solution, rinsing twice, mixing concentrated solution and rinsing solution to 66L, cleaning the equipment, collecting total treatment time of 148min, mixing 66L total concentrated solution, sampling, detecting (no visible thallus precipitate after centrifugation, enzyme activity of 160L total permeation solution hyaluronidase is 19672U/ml, enzyme activity of 66L total concentrated solution hyaluronidase is 9.98 × 10) 5 U/ml)。
Proved by verification, 146L of leech hyaluronidase fermentation liquor is prepared into purified hyaluronidase liquor (no visible thalli after centrifugation) by the process, and the enzyme activity is 9.98 multiplied by 10 5 U/ml (enzyme activity loss is about 29%, and the enzyme activity detection value is detected under the same condition), the low-pressure ceramic membrane treatment time is about 246min, and the high-pressure ceramic ultrafiltration membrane treatment time is about 148min.
Verified by the above example 1,2,3
In example 1, 200nm is selected for the low-pressure ceramic membrane sterilization process, the treatment time is about 136min, 15000Da is selected for the high-pressure ceramic ultrafiltration membrane impurity removal process, the treatment time is about 274min, and the enzyme activity loss is about 22%.
In the embodiment 2, the low-pressure ceramic membrane sterilization process is 200nm, the processing time is about 168min, the high-pressure ceramic ultrafiltration membrane impurity removal process is 25000Da, the processing time is about 196min, and the enzyme activity loss is about 39%.
In example 3, the low-pressure ceramic membrane sterilization process is selected to be 50nm, the processing time is about 246min, the high-pressure ceramic ultrafiltration membrane impurity removal process is selected to be 15000Da, the processing time is about 148min, and the enzyme activity loss is about 29%.
The detection values (including all process samples) of the embodiments 1 and 2 can verify that the high-pressure ceramic ultrafiltration membrane has large aperture and large material loss under approximately equal conditions, and is verified by multiple experiments.
The detection values (including all process samples) of the embodiments 1 and 3 can verify that the low-pressure ceramic membrane under approximately equal conditions has large pore diameter, short treatment time and is verified by multiple experiments.
The verification shows that the low-pressure ceramic membrane sterilization process is 200nm, the high-pressure ceramic ultrafiltration membrane impurity removal process is 15000Da, the production efficiency is high, and the enzyme activity loss is low.
Table 1 is a table of data for example 1,2,3
Comparative example 1
Comparative example 1 differs from example 1 in that the remaining 140L of the fermentation broth from example 1 was sterilized by plate and frame sterilization, low pressure ceramic membrane sterilization (in accordance with the conditions of example 1) to give about 132L of hyaluronidase clear solution, and 66L of the clear solution after low pressure ceramic membrane sterilization was applied to a 10K organic ultrafiltration membrane (designed to have a membrane area of about 0.75 m) 2 Three 1812 membranes are connected in parallel) to remove impurities, the operating pressure is controlled to be 0.32Mpa (the designed using pressure for treating materials is 0.30-0.35Mpa, the pressure is selected to be the best stability for treating the materials by an industrial organic ultrafiltration membrane), the temperature of the material liquid is controlled to be 30-35 ℃, 2% sodium chloride solution is added for continuous flow dialysis when the materials are concentrated to about 20L, the membranes are blocked when less than 10L of saline is added for dialysis, and the tail line of the permeation liquid is darker in color. The total permeate was about 53L. Collecting the concentrated solution, adding 2% sodium chloride solution, rinsing twice, mixing the concentrated solution and the rinsing solution to 66L, stopping cleaning equipment, performing total treatment for 165min, mixing the 66L total concentrated solution, sampling, and detecting (no macroscopic thalli precipitation after centrifugation, enzyme activity loss is about 27%).
Comparative example 2
Comparative example 2 differs from example 1 and comparative example 1 in that the remaining 66L of the low pressure ceramic membrane from comparative example 1 was sterilized and the supernatant was applied to a 20K organic ultrafiltration membrane (designed to have a membrane area of about 0.75 m) 2 Three 1812 membranes are connected in parallel) to remove impurities, the operating pressure is controlled to be 0.32Mpa (the designed using pressure for treating materials is 0.30-0.35Mpa, the pressure is the best stability for treating the materials by an industrial organic ultrafiltration membrane), the temperature of the material liquid is controlled to be 30-35 ℃, 2% sodium chloride solution is added for continuous flow dialysis when the materials are concentrated to about 20L, the membranes are blocked when about 14L of saline is added for dialysis, and the tail line of the permeation liquid is darker in color. The total permeate was about 60L. Collecting concentrated solution, adding 2% sodium chloride solution, rinsing twice, mixing concentrated solution and rinsing solution to 66L, stopping cleaning equipment, and treatingAnd (4) mixing the 66L total concentrated solution uniformly, sampling and detecting (no macroscopic thalli precipitation exists after centrifugation, and the enzyme activity loss is about 37%).
It is verified from the above example 1 and comparative example 1 that when the hyaluronidase solution is treated under the same conditions (the area of the organic ultrafiltration membrane is larger than that of the high-pressure ceramic ultrafiltration membrane), the ceramic ultrafiltration membrane has a large treatment capacity and is more stable.
Compared with the 10K organic ultrafiltration membrane, the 20K organic ultrafiltration membrane has the advantages of high efficiency and high loss in treating the hyaluronidase liquid, which is verified by the comparative example 1 and the comparative example 2.
From the above example 1 and comparative examples 1 and 2, it was confirmed that when the hyaluronidase solution was treated under the same conditions, the ceramic ultrafiltration membrane had a larger treatment amount and was more stable than the organic ultrafiltration membrane (multiple experimental verifications).
Table 2 is a table of data for example 1 and comparative example 1,2, above
Comparative example 3
Comparative example 3 is different from example 1 in that the high pressure ceramic ultrafiltration membrane is operated at a pressure of 0.90Mpa (a pressure of 0.85 to 0.90Mpa during operation), and the other conditions are the same as example 1. The low-pressure ceramic membrane sterilization treatment time is about 146min, the high-pressure ceramic ultrafiltration membrane impurity removal treatment time is about 258min, the purified enzyme solution is centrifuged, the precipitation of thalli can not be seen by naked eyes, and the activity loss is about 28%.
The embodiment 1 and the comparative example 3 prove that the operating pressure of the high-pressure ceramic ultrafiltration membrane is 0.90Mpa, compared with the operating pressure of 0.70Mpa, the operating time and the enzyme activity loss (verified by multiple tests) have no significant influence, and the energy consumption is higher when the operating pressure of the high-pressure ceramic ultrafiltration membrane is increased.
Comparative example 4
Comparative example 4 is different from example 1 and comparative example 3 in that the high pressure ceramic ultrafiltration membrane is operated at a pressure of 0.55Mpa (a pressure between 0.50 and 0.55Mpa during operation), and other conditions are the same as those of example 1 and comparative example 3. The low-pressure ceramic membrane sterilization treatment time is about 157min, the high-pressure ceramic ultrafiltration membrane impurity removal treatment time is about 326min, the purified enzyme solution is centrifuged, the precipitation of thalli can not be seen by naked eyes, and the enzyme activity loss is about 26%.
The operation pressure of the high-pressure ceramic ultrafiltration membrane is below 0.90Mpa, the purified enzyme liquid is centrifuged without macroscopic thalli precipitation, the enzyme activity loss (verified by the process sample enzyme activity and results of multiple tests) is not significantly influenced, and the operation pressure of the high-pressure ceramic ultrafiltration membrane for treating the hyaluronidase liquid with the production efficiency is 0.7Mpa, which is the optimal operation pressure (according with the operation rule of the high-pressure ceramic ultrafiltration membrane for treating materials).
Table 3 is a table of data for example 1 and comparative example 3,4, above
Comparative example 5
Comparative example 5 is different from example 1 in that the sodium chloride solution as a buffer salt was changed to pure water, and other conditions were the same as example 1. The time of the low-pressure ceramic membrane sterilization treatment is about 164min, trace thalli precipitation is generated in the centrifugation of the total permeate of the low-pressure ceramic membrane, the time of the high-pressure ceramic ultrafiltration membrane impurity removal treatment is about 367min, the thalli precipitation is generated in the centrifugation of the purified enzyme liquid, and the enzyme activity loss is about 34%.
Comparative example 6
Comparative example 6 differs from examples 1 and 5 in that the concentration of the buffer salt sodium chloride solution was 1%, and the other conditions were the same as in examples 1 and 5. The sterilization treatment time of the low-pressure ceramic membrane is about 139min, trace visible thallus precipitates are obtained by centrifuging the total permeate of the low-pressure ceramic membrane, the impurity removal treatment time of the high-pressure ceramic ultrafiltration membrane is about 295min, trace thallus precipitates are obtained by centrifuging the purified enzyme solution, and the enzyme activity loss is about 25%.
Comparative example 7
Comparative example 7 differs from example 1 and comparative examples 5 and 6 in that the concentration of the buffered saline sodium chloride solution was 3%, and the other conditions were the same as in example 1 and comparative examples 5 and 6. The sterilization treatment time of the low-pressure ceramic membrane is about 151min, the total permeate of the low-pressure ceramic membrane is centrifuged without visible precipitation, the impurity removal treatment time of the high-pressure ceramic ultrafiltration membrane is about 265min, the purified enzyme solution is centrifuged with trace thalli precipitation, and the enzyme activity loss is about 27%.
Verified by the above example 1 and comparative example 5, and comparative example 6 and comparative example 7, the concentration of the buffer salt sodium chloride solution is 0,1%, and the purified enzyme solution is centrifuged to have a bacterial precipitate; the concentration of the buffer salt sodium chloride solution is 2%, the enzyme liquid is subjected to centrifugal aseptic precipitation after 3% purification (the enzyme liquid is easy to be infected with bacteria in the production process, and a certain buffer salt sodium chloride solution has the function of inhibiting bacterial colony propagation), the enzyme activity loss has no significant influence (except the buffer salt sodium chloride solution with the concentration of 0), and the optimal concentration of the buffer salt sodium chloride solution is 2% by combining the condition of centrifugal bacteria after the enzyme liquid is purified and the production cost.
Table 4 is a table of data for example 1 and comparative example 5,6,7, above
Comparative example 8
Comparative example 8 is different from example 1 in that the temperature of the material is controlled to 25 ℃ to 30 ℃ and other conditions are the same as example 1. The low-pressure ceramic membrane sterilization treatment time is about 174min, the total permeate of the low-pressure ceramic membrane is centrifuged without macroscopic thalli precipitation, the high-pressure ceramic ultrafiltration membrane impurity removal treatment time is about 341min, the purified enzyme solution is centrifuged without macroscopic thalli precipitation, and the enzyme activity loss is about 23%.
Comparative example 9
Comparative example 9 is different from example 1 and comparative example 8 in that the temperature of the material is controlled to 35 ℃ to 40 ℃ and other conditions are the same as example 1. The sterilization treatment time of the low-pressure ceramic membrane is about 128min, trace visible thallus precipitates are centrifuged in the total permeate of the low-pressure ceramic membrane, the impurity removal treatment time of the high-pressure ceramic ultrafiltration membrane is about 260min, trace thallus precipitates are centrifuged in the purified enzyme liquid, and the enzyme activity loss is about 30%.
The experiment results of the example 1 and the comparative example 8 prove that the hyaluronidase liquid is treated under the same conditions, the material temperature is controlled to be 30-35 ℃ and is 25-30 ℃, the production efficiency is high, the enzyme activity loss has no significant difference, and the enzyme liquid after purification has no visible precipitation after centrifugation.
The experiment 1 and the comparative example 9 prove that the hyaluronidase liquid is treated under the same conditions, the material temperature is controlled to be 30-35 ℃ compared with 35-40 ℃, the production efficiency and the enzyme activity loss have no significant difference, and the centrifugal thallus precipitation of the purified enzyme liquid is less (thallus is easily generated in the production process after the temperature is increased).
The experiment of example 1, the comparison example 8 and the comparison example 9 proves that the material temperature is controlled to be 30-35 ℃ which is the optimal material temperature by combining the production efficiency and the condition of centrifugal thallus precipitation of the purified enzyme liquid.
Table 5 is a table of data for example 1 and comparative example 8,9, above
According to the embodiment, the comparative example, the data table and the multiple production verification, the industrial purification of the leech hyaluronidase adopts the plate-and-frame pure bacteria, the 200nm low-pressure ceramic membrane pure bacteria and the 15000Da high-pressure ceramic ultrafiltration membrane impurity removal production process, the material temperature is controlled to be 30-35 ℃, the buffer salt solution adopts a 2% sodium chloride solution feeding mode, the enzyme activity loss of the produced leech hyaluronidase is low, the production cost is low, the efficiency is high, the enzyme solution is less in thallus, no additional impurity is introduced in the continuous production of enzyme digestion ultra-small molecular hyaluronic acid, the quality of the enzyme digestion ultra-small molecular hyaluronic acid product is improved, and the method is suitable for the continuous production of the enzyme digestion ultra-small molecular hyaluronic acid.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (10)
1. A method for purifying hyaluronidase comprising the steps of:
a) Sterilizing the hyaluronidase fermentation broth by using a plate frame to obtain a hyaluronidase clear liquid;
b) Sterilizing the hyaluronidase clear liquid by adopting a low-pressure ceramic membrane to obtain hyaluronidase liquid treated by the low-pressure ceramic membrane;
c) And removing impurities from the hyaluronidase liquid treated by the low-pressure ceramic membrane by using a high-pressure ceramic ultrafiltration membrane to obtain the hyaluronidase.
2. The method of claim 1, wherein the hyaluronidase source of step a) is a leech; the mass content of the thalli in the hyaluronidase fermentation broth is 50-55 wt%.
3. The method according to claim 1, wherein the mass content of the thalli in the hyaluronidase clear liquid in step A) is 1-5 wt%;
the enzyme activity of the hyaluronidase clear liquid is 1.2 multiplied by 10 6 ～1.6×10 6 U/ml。
4. The method according to claim 1, wherein the low pressure ceramic membrane of step B) has a gauge of 50 to 200nm; the membrane area of the low-pressure ceramic membrane is 0.286 square meter, the equipment design pressure is 0.3-0.35 Mpa, and the material liquid temperature is 30-35 ℃.
5. The method according to claim 1, wherein the low pressure ceramic membrane is sterilized in step B), followed by adding buffer salt in a continuous flow manner, and dialyzing to obtain a low pressure ceramic membrane-treated hyaluronidase solution; the enzyme activity of the hyaluronidase liquid treated by the low-pressure ceramic membrane is 5 multiplied by 10 5 ～7×10 5 U/ml; the buffer salt is 1-3% sodium chloride solution.
6. The method of claim 1, wherein the high pressure ceramic ultrafiltration membrane of step C) has a specification of 15000 to 25000Da; the membrane area of the high-pressure ceramic ultrafiltration membrane is 0.286 square meter, the design pressure of the equipment is 0.5-0.9 Mpa, the pressure of the equipment in operation is 0.70-0.75 Mpa, and the temperature of the feed liquid is 30-35 ℃.
7. The method according to claim 1, wherein after the high-pressure ceramic membrane is subjected to impurity removal in the step C), buffer salt is added in a continuous flow addition manner, and the mixture is dialyzed until the concentration of a tail line of the permeate and the buffer salt solution is consistent, and then the mixture is continuously added until the permeate is colorless; the buffer salt is 1-3% sodium chloride solution.
8. The method of claim 1, wherein the low pressure ceramic membrane has a gauge of 200nm and the high pressure ceramic membrane has a gauge of 15000Da.
9. A hyaluronidase which is produced by the production method according to any one of claims 1 to 9.
10. Use of the hyaluronidase produced by the method of any one of claims 1-9 in the production of a hyaluronic acid degradation product.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211108780.2A CN115287275B (en) | 2022-09-13 | 2022-09-13 | Method for purifying hyaluronidase |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211108780.2A CN115287275B (en) | 2022-09-13 | 2022-09-13 | Method for purifying hyaluronidase |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN115287275A true CN115287275A (en) | 2022-11-04 |
| CN115287275B CN115287275B (en) | 2024-03-15 |
Family
ID=83833986
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202211108780.2A Active CN115287275B (en) | 2022-09-13 | 2022-09-13 | Method for purifying hyaluronidase |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN115287275B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116023523A (en) * | 2022-12-29 | 2023-04-28 | 水羊化妆品制造有限公司 | Ultra-small molecular weight sodium hyaluronate and preparation method thereof |
| CN117165558A (en) * | 2023-09-27 | 2023-12-05 | 四川德博尔制药有限公司 | Preparation method of hyaluronidase |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20060172967A1 (en) * | 2005-01-31 | 2006-08-03 | Seikagaku Corporation | Method for producing alkyl-esterified glycosaminoglycan |
| CN101313913A (en) * | 2008-01-29 | 2008-12-03 | 杏辉天力（杭州）药业有限公司 | Hyaluronate lyase restrainer |
| CN104140952A (en) * | 2014-08-08 | 2014-11-12 | 山东威高新生医疗器械有限公司 | Hyaluronidase and preparation method thereof |
-
2022
- 2022-09-13 CN CN202211108780.2A patent/CN115287275B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20060172967A1 (en) * | 2005-01-31 | 2006-08-03 | Seikagaku Corporation | Method for producing alkyl-esterified glycosaminoglycan |
| CN101313913A (en) * | 2008-01-29 | 2008-12-03 | 杏辉天力（杭州）药业有限公司 | Hyaluronate lyase restrainer |
| CN104140952A (en) * | 2014-08-08 | 2014-11-12 | 山东威高新生医疗器械有限公司 | Hyaluronidase and preparation method thereof |
Non-Patent Citations (1)
| Title |
|---|
| 谷劲松, 许平, 李铁林, 曲音波: "乳酸氧化酶转化乳酸产丙酮酸", 应用与环境生物学报, no. 06 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116023523A (en) * | 2022-12-29 | 2023-04-28 | 水羊化妆品制造有限公司 | Ultra-small molecular weight sodium hyaluronate and preparation method thereof |
| CN117165558A (en) * | 2023-09-27 | 2023-12-05 | 四川德博尔制药有限公司 | Preparation method of hyaluronidase |
Also Published As
| Publication number | Publication date |
|---|---|
| CN115287275B (en) | 2024-03-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| KR101509139B1 (en) | Method for purifying hyaluronic acid | |
| CN102639722B (en) | The manufacture method of liquid glucose | |
| EP3730623A1 (en) | Small-molecule hyaluronic acid or salt thereof, and preparation method therefor | |
| CN115287275A (en) | Method for purifying hyaluronidase | |
| CN102961741B (en) | Method for preparing tetanus toxoid vaccine | |
| Iwasaki et al. | Purification of pectate oligosaccharides showing root-growth-promoting activity in lettuce using ultrafiltration and nanofiltration membranes | |
| CN103613753A (en) | Method for separating and purifying polyglutamic acid by using additive-free organic solvent | |
| CA1244368A (en) | Processing of a heteropolysaccharides solution; heteropolysaccharides powder compositions and their use | |
| CN113373134B (en) | Extraction method of N-acetylglucosamine deacetylase | |
| CN113151336B (en) | Method for constructing hyaluronic acid engineering strain by recombinant expression plasmid and application | |
| CN113454204B (en) | Method for extracting phycocyanin | |
| CN114525263A (en) | Purification and concentration method of porcine acute diarrhea syndrome coronavirus antigen | |
| JP2763112B2 (en) | Water-soluble low molecular weight chitosan and method for producing the same | |
| JP3899462B2 (en) | Cancer cell apoptosis inducer | |
| JP2559683B2 (en) | Bacterial cellulose-containing filtration membrane | |
| JPH0265789A (en) | Production of agar oligosaccharide | |
| RU2584601C1 (en) | Method of extracting proteolytic terrilytin enzyme | |
| JPH0219393A (en) | N-acetylogalactosaminooligosaccahride and production thereof | |
| RU2822178C2 (en) | Method of extracting phycocyanins | |
| JP2009284826A (en) | Method for producing hyaluronic acid | |
| KR100253423B1 (en) | Process for purifying erythritol | |
| CN117756958A (en) | Method for preparing streptococcus pneumoniae capsular polysaccharide or polysaccharide degradation thereof | |
| CN116555375A (en) | Preparation method and application of hyaluronic acid oligosaccharide | |
| JPS6040831B2 (en) | Processing method for microbial culture solution | |
| CN116179629A (en) | Preparation method of unsaturated sodium hyaluronate disaccharide |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |